CN103285609A - Heat exchange distillation apparatus - Google Patents
Heat exchange distillation apparatus Download PDFInfo
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- CN103285609A CN103285609A CN2013100434985A CN201310043498A CN103285609A CN 103285609 A CN103285609 A CN 103285609A CN 2013100434985 A CN2013100434985 A CN 2013100434985A CN 201310043498 A CN201310043498 A CN 201310043498A CN 103285609 A CN103285609 A CN 103285609A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/26—Fractionating columns in which vapour and liquid flow past each other, or in which the fluid is sprayed into the vapour, or in which a two-phase mixture is passed in one direction
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
- B01D3/4261—Side stream
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- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a heat exchange distillation apparatus. The distillation apparatus according to the present invention includes a rectifying column, a stripping column located above seen from the rectifying column, a liquid sump unit located at a predetermined stage of the stripping column and configured to hold liquid that has flowed downward, a heat exchanger located in the liquid sump unit, a second pipe for introducing vapor in the rectifying column to the heat exchanger of the stripping column, and a third pipe for introducing fluids flowing out from the heat exchanger of the stripping column to the rectifying column. Further, a flare line having lower pressure than pressure in the rectifying column is connected to a downstream side of the third pipe. The distillation apparatus can switch a first flow toward an inside of the rectifying column through the third pipe to a second flow branching from the third pipe toward a pipe at a lower pressure side. The apparatus configuration can achieve further energy saving and reduction in manufacturing cost.
Description
Technical field
The present invention relates to a kind of distilling apparatus for the distillation procedure of implementing to be widely used in many industrial flows, relate in particular to a kind of heat exchange type distilling apparatus.
Background technology
The separated operation generally is widely used in industrial flow, but also is that energy consumes very large unit operations.Therefore in industrial circle, carrying out to reduce the research of the distilling apparatus that energy consumes.In such research, as the distilling apparatus of energy saving excellence, carrying out the exploitation of internal heat exchange type destilling tower (Heat Integrated Distillation Column is hereinafter referred to as HIDiC).
The fundamental system of this HIDiC has concentrated portion (high-voltage section) is separated structure arranged with recoverer (low voltage section) as shown in Figure 1.And, for the operating temperature that makes the portion that concentrates is higher than the operating temperature of recoverer, and make the operating pressure of the portion of concentrating be higher than the operating pressure of recoverer.Thus, if having heat-exchange surface between the two, then produce hot the movement from concentrating portion to recoverer, therefore can reduce the hot input quantity of reboiler.And because the heat of the portion of concentrating moves to recoverer, therefore can reduce the heat that removes of condenser.Therefore, become the high distilling apparatus of energy efficiency.
In order to realize the practicability of this HIDiC, the distilling apparatus of multiple double-sleeve structure has been proposed, this double-sleeve structure is made of (for example with reference to patent documentation 1: TOHKEMY 2004-16928 communique) the interior pipe that forms the portion of concentrating and the outer tube that forms recoverer.Such structure is because to produce heat to recoverer (outer tube) mobile from concentrating portion's (interior pipe), therefore can reduce in hot input quantity in the reboiler and the condenser except heat.
Yet, as disclosure described in Patent Document 1, concentrate heat exchange type distilling apparatus that portion and recoverer construct with double-sleeve structure and have following 1)～6) problem.
1) side that can't carry out product is heated up in a steamer (side cut).Side is heated up in a steamer product in the distillation flowchart process that refers to finally to be distillated before the product and is extracted situation as the intermediate fractionation product out.
In the distilling apparatus of patent documentation 1 record, the pipe unit group of double-sleeve structure is disposed in the mode of joining each other.And, to outer tube and interior pipe fill rule filler.Therefore, the mode that can't take out the intermediate fractionation product with the interior pipe from each pipe unit forms pipe arrangement, can't realize that consequently side heats up in a steamer.
2) can't carry out the optimization of raw material supplying section (feeding section).This is because in the concentrated portion of being constructed by double-sleeve structure and recoverer, loading separately is identical, can't freely set the hop count of the portion of concentrating and recoverer.
3) can't change the supply position corresponding to the raw material of supplying with.This is because as above-mentioned 2) as described in can't freely set the cause of the structure of feeding fragment position.
4) can't tackle polynary feeding (acceptance of a plurality of feed streams).This is because as above-mentioned 1) as described in can't be to the cause of the structure of base feed in the way of dual pipe.
5) device is difficult in maintenance.As above-mentioned 1) as described in owing to used the pipe unit of regular filler adjacent one another are and intensive, therefore can't be fully near desirable pipe unit, thereby can't carry out their maintenance.
6) used the concentrated portion of dual pipe and the heat exchange amount between the recoverer not to have the free degree in the design with respect to heat transfer area, only depended on the Temperature Distribution of destilling tower, the free degree in the device design in the design of heat exchange amount is little.
Be U in overall heat-transfer coefficient, heat transfer area is A, and when concentrating temperature difference between portion and the recoverer and being Δ T, the heat exchange amount Q that concentrates between portion and the recoverer is represented by Q=U * A * Δ T.In the HIDiC that has used double-sleeve structure, the inner tubal wall face becomes heat transfer area.This heat transfer area is the fixed value according to the shape decision of dual pipe.About overall heat-transfer coefficient, be according to heat transfer structure and carry out the fixed value that the physical properties of fluids of heat exchange determines.Therefore, calculate formula as can be known from above-mentioned heat exchange amount, the heat exchange amount during design can only change according to the concentrated portion that changes because of the operating pressure that concentrates portion and recoverer and the temperature difference between the recoverer.
As the heat exchange type distilling apparatus that can solve above-mentioned problem, the applicant has proposed patent documentation 2: the scheme that No. the 4803470th, Japan Patent.
Fig. 2 represents an example of patent documentation 2 disclosed distilling apparatus.This distilling apparatus possesses: concentration tower 1; Be configured in the locational recovery tower 2 higher than concentration tower 1; First pipe arrangement 23 that the top of tower 2c of recovery tower is communicated with the tower bottom 1a of concentration tower; The compressor reducer 4 that steam from the top of tower 2c of recovery tower is compressed and transmits to the tower bottom 1a of concentration tower.And distilling apparatus possesses: the section that is arranged on the regulation of recovery tower 2 goes up, accumulates the 2e of hydrops portion of the liquid that flows down from the top; Be configured in the heat exchanger 8 in the 2e of hydrops portion; The demarcation strip 16 that is arranged on the position of regulation of concentration tower 1 and will section up and down separates fully; Second pipe arrangement 29 that the steam heat exchanger 8 of the downside of demarcation strip 16 is imported; The 3rd pipe arrangement 30 that the fluid that will flow out from heat exchanger 8 after will importing via second pipe arrangement, 29 heat exchanger 8 imports to the upside of demarcation strip 16.
In such structure, utilize second pipe arrangement 29 that the steam in the concentration tower 1 is extracted out outside tower, this steam is imported to the heat exchanger 8 in the recovery tower 2, thereby the heat of concentration tower 1 is moved to recovery tower 2.And the HCS in the concentration tower 1 rises in second pipe arrangement 29 towards the heat exchanger 8 of recovery tower 2, and thus, part or all fluid that condensation taken place is by from three pipe arrangement 30 extrusion of recovery tower 2 outside tower heat exchanger 8 in.Therefore, this structure does not need pump equal pressure conveying mechanism the liquor charging of the concentration tower to the vertical downside 1 from recovery tower 2.
In addition, above-mentioned use second pipe arrangement 29, the 3rd pipe arrangement 30 and heat exchanger 8 and from concentration tower 1 to recovery tower 2 distilling apparatus that carry out the mobile apparatus structures of the heat structure mobile with not possessing this heat compare, can reduce the condenser 7 installed at the top of tower of concentration tower 1 except heat, and, also can reduce the hot input quantity of the reboiler 3 installed at the tower bottom of recovery tower 2.The result is to provide a kind of energy efficiency good distilling apparatus.
In addition owing to can use the plate column portion identical with common distilling apparatus or packed column portion to constitute concentration tower 1 or recovery tower 2, therefore side heat up in a steamer or the enforcement of polynary feeding in especially improved device just can tackle, and the maintenance of installing is also easy.And from same reason, the setting of the hop count of concentration tower or recovery tower has the free degree, can carry out the optimization of raw material supplying section.
In addition, because heat transfer area becomes the free degree of design, therefore can not rely on decision heat exchange amount in temperature difference ground in the tower.
As described above, according to the device example (Fig. 2) of patent documentation 2 record, the energy efficiency excellence can easily be answered enforcement that offside heats up in a steamer or the setting of feeding fragment position, and the maintenance of device is also easy.And device of the present invention becomes the apparatus structure of the free degree increase of design, is therefore accepted by user one side easily.
Yet the present application person are target for distilling apparatus shown in Figure 2 with the further raising of energy efficiency and by the more acceptable structure of user one side, have considered the problem that should solve that also exists in this distilling apparatus.
That is, in distilling apparatus shown in Figure 2, adopt following method.The demarcation strip of separating fully along above-below direction in the section arbitrarily of concentration tower 1, arranging tower 16, outside tower, extracted out by pipe arrangement 29 from the whole steam that rises in the below of demarcation strip 16, the heat exchanger 8 of the tube bank type on the section arbitrarily that is arranged on recovery tower 2 is supplied with, and carries out heat exchange at this.Then, part or all fluid that condensation taken place flows by the top of the demarcation strip 16 of gravity in the concentration tower 1 via the pipe arrangement 30 outside the tower in heat exchanger 8, and condensed liquid can move to the below of demarcation strip 16 via another pipe arrangement 31.Thereby carry out the circulation of such fluid.
In this method, because supposition is extracted the whole steam in the concentration tower 1 out outside tower, therefore become demarcation strip 16 to be set in concentration tower 1 and to make from recovery tower 2 and be sent to condensate liquid on the demarcation strip 16 further moves such complexity to the lower side space of demarcation strip 16 via the pipe arrangement 31 outside the tower and control valve 17 structure.Thus, on the viewpoint of structure and manufacturing cost, also there is the problem that to improve.
In addition, by giving the pressure loss up and down at demarcation strip 16, obtain the driving force of the fluid of the pipe by heat exchanger 8, therefore correspondingly, need make the pressure of the pressure ratio top of tower 1c of the tower bottom 1a that concentrates portion 1 increase the pressure loss amount up and down of dividing plate 16.Thus, need be with the lifting capacity (being increasing compression ratio) of the pressure of this tower bottom of outlet side boost in pressure 1a side of compressor reducer 4.Therefore, there is amendatory problem in the viewpoint in energy saving.
Summary of the invention
The present invention makes in view of above-mentioned problem, and its purpose is in above-mentioned distilling apparatus (Fig. 2), realizes the minimizing of further energy-conservationization and manufacturing cost.
The heat exchange type distilling apparatus of a mode of the present invention possesses: concentration tower, and it is the tower body that is utilized as the portion that concentrates and has plate column portion or packed column portion; Recovery tower, it is configured in the top when observing from concentration tower, is the tower body that is utilized as recoverer and has plate column portion or packed column portion; First pipe arrangement, it makes the top of tower of recovery tower be communicated with the tower bottom of concentration tower; Compressor reducer, it is arranged at first pipe arrangement, and the steam from the top of tower of recovery tower is compressed and transmits to the tower bottom of concentration tower.And then this mode has: hydrops portion, its be arranged on recovery tower regulation the section on, accumulate the liquid that flows down from the top; Heat exchanger, it is configured in the hydrops portion of recovery tower; Second pipe arrangement, it imports the heat exchanger of the steam in the concentration tower to recovery tower; The 3rd pipe arrangement, its fluid that will flow out from the heat exchanger of recovery tower imports to concentration tower.
In such mode, by second pipe arrangement part of the steam in the concentration tower is extracted out outside tower, the volume contraction of utilizing heat exchanger 8 in the recovery tower to make the whole condensations of this steam and producing becomes driving force, can obtain from concentration tower to recovery tower and then the flowing of the fluid from recovery tower to concentration tower.Therefore, do not need pump equal pressure conveying mechanism.
In the present invention, because the plate (demarcation strip 16 of Fig. 2) that section is up and down separated fully is not set in concentration tower 1, therefore compare with the distilling apparatus of Fig. 2, because this demarcation strip is not set, therefore can correspondingly reduce the pressure loss in the portion of concentrating, can reduce concentration tower the tower bottom side pressure and must be lower with the outlet side pressure restraining of compressor reducer.Therefore, energy saving improves.And structure is also simplified.
In addition, use second to carry out the mobile apparatus structure of heat from concentration tower to recovery tower with the 3rd pipe arrangement and heat exchanger and compare with the distilling apparatus that does not possess this hot moving structure as described above, can reduce the condenser installed at the top of tower of concentration tower except heat, and, also can reduce the hot input quantity of the reboiler installed at the tower bottom of recovery tower.The result is to provide a kind of energy efficiency high distilling apparatus.
In addition because concentration tower or recovery tower use the plate column portion identical with common distilling apparatus or packed column portion to constitute, therefore side heat up in a steamer or the enforcement of polynary feeding in need not just improve and can tackle device especially, and the maintenance of installing is also easy.And from same reason, in the setting of the hop count of concentration tower or recovery tower, have the free degree, can carry out the optimization of raw material supplying section.
And, because heat transfer area becomes the free degree of design, therefore can not rely on the interior temperature difference of tower and decide heat exchange amount.
In addition, in the present invention, link the pipeline with pressure lower than the pressure in the concentration tower in the downstream of the 3rd pipe arrangement.So, can be with first the flowing and to switch to from the 3rd pipe arrangement branch and flow towards second of described pipeline in concentration tower by the 3rd pipe arrangement.
This be because, when because the pressure oscillations in the distilling apparatus running etc. are former thereby when making the state that becomes in the end that is inserted into the 3rd pipe arrangement in the concentration tower not by the liquid sealing, steam flows in the 3rd pipe arrangement in concentration tower sometimes, and possibly can't construct above-mentioned first flows.Therefore, when not sealed by liquid in the end of the 3rd pipe arrangement in being inserted into concentration tower, the valve of being located at the 3rd pipe arrangement cuts out, flow from first and to switch to second and flow, thus, the pressure differential between utilizing in pipeline with pressure lower than the pressure in the concentration tower and the concentration tower is forcibly introduced steam in second pipe arrangement in concentration tower, condensate liquid can be accumulated in the 3rd pipe arrangement, thereby can make the first above-mentioned mobile regeneration.Thus, can establish circulation in the stable side heat exchange.
According to the present invention, the energy efficiency excellence can easily be answered enforcement that offside heats up in a steamer or the setting of feeding fragment position, and the maintenance of device is also easy.And device of the present invention becomes the apparatus structure of the free degree increase of design, is therefore accepted by user one side easily.
And, according to the present invention, can realize the minimizing of further energy-conservationization and manufacturing cost.
Description of drawings
Fig. 1 is the figure of the basic structure of expression HIDiC.
Fig. 2 is that the expression formerly technology related with the application is the brief configuration figure of an example of patent documentation 2 disclosed distilling apparatus.
Fig. 3 is the overall structure figure of the heat exchange type distilling apparatus of one embodiment of the present invention.
Fig. 4 is the figure that is illustrated in the peripheral structure of the tube bank type heat exchanger that disposes in the recovery tower of Fig. 3.
[symbol description]
1 concentration tower
The 1a tower bottom
1b plate column portion (or packed column portion)
The 1c top of tower
2 recovery towers
The 2a tower bottom
2b plate column portion (or packed column portion)
The 2c top of tower
2d drawing liquid portion
2e hydrops portion
3 heaters (reboiler)
4 compressor reducers
5 shelves
6 pressure conveying mechanisms
7 condensers (condenser)
8 tube bank type heat exchangers
5,15 hydrops shelves
9 hydrops pallets
10,12,14 liquid
11,13,18 steams (vapor)
21,22,23,24,25,26,27,28,29,30,44 pipe arrangements
The outlet of 30a pipe arrangement
42,45 valves
43 flare lines (Off レ ア one ラ イ Application)
46 MA monitoring agencies
The specific embodiment
The essential characteristic of heat exchange type distilling apparatus of the present invention is to be respectively equipped with the tower body (recovery tower) that is utilized as the recoverer that extends along vertical and the tower body (concentration tower) that is utilized as the concentrated portion of extending along vertical, and recovery tower is configured on the position than concentrated tower height.Need to prove, the common distilling apparatus that is not the internal heat exchange type is made of tower, this tower is to constitute along the tower of vertical construction and by tower bottom, plate column portion (or packed column portion) and top of tower, plate column portion (or packed column portion) is the border with the raw material supplying position, upside is for concentrating portion, downside is recoverer, and is different fully with heat exchange type distilling apparatus of the present invention.The mode of especially following explanation has applied improvement to the distilling apparatus of Fig. 2 that the applicant proposes.Therefore, for the structure identical with structural element shown in Figure 2, use prosign that the embodiments of the present invention example is described.
Fig. 3 represents the overall structure figure of the heat exchange type distilling apparatus of one embodiment of the present invention.The heat exchange type distilling apparatus of present embodiment has concentration tower 1, be configured in the locational recovery tower 2 higher than concentration tower 1.Concentration tower 1 is made of tower bottom 1a, the 1b of plate column portion (or packed column portion), top of tower 1c.Recovery tower 2 also is made of tower bottom 2a, the 2b of plate column portion (or packed column portion), top of tower 2c.
The 1b of plate column portion, 2b are the towers of the type of the shelf (pallet) that is provided with several levels in tower.With the space section of being called between each shelf.In each section, promote the gas-liquid contact and carry out the result that material moves to be, the gas phase section upward that is rich in the higher composition of volatility is transmitted, the liquid phase section downwards that is rich in the lower composition of volatility is wandered, carried out with new liquid phase or gas phase that gas-liquid contacts again and carry out material and move.Like this, more lean on the Duan Yue on the top of tower to be rich in the high composition of volatility, more the Duan Yue of portion is rich in the low composition of volatility on the lower, carries out distillation procedure thus.
The packed column portion that can be replaced into plate column portion puts into some filler in the tower of hollow, and carries out the tower of the type of gas-liquid contact on its surface.By with plate column portion identical mechanism, more more be rich in the high composition of volatility by the top of tower, the low composition of volatility more is rich in portion more on the lower, carries out distillation procedure thus.
In Fig. 3, though the inside of the 1b of plate column portion, 2b (or packed column portion) is depicted blank as, in fact adopt structure as described above.
And, about concentration tower 1 and recovery tower 2, be described in detail respectively.At first, recovery tower 2 is described.
The outside at the tower bottom 2a of recovery tower 2 is equipped with the heater 3 that is called as reboiler, and pipe arrangement 21 arranges via the space top of heater 3 to tower bottom 2a from the bottom, space of tower bottom 2a.Therefore, the liquid that flows down in the 2b of plate column portion of recovery tower 2 (or packed column portion) accumulates in tower bottom 2a, and the part of this liquid becomes steam by heater 3 heating, returns tower bottom 2a.And, obtain being rich in the raffinate of the low composition of volatility by pipe arrangement 22 from the bottommost of tower bottom 2a.
The top of tower 2c of recovery tower 2 becomes the position of base feed.Top of tower 2c uses pipe arrangement 23 to be connected with the tower bottom 1a of concentration tower 1 via compressor reducer 4.In the present embodiment, though the raw material supplying position is made as the top of tower 2c of recovery tower 2, the raw material supplying position also can be the section arbitrarily of the 2b of plate column portion (or packed column portion).And, having under the situation of plurality of raw materials, the raw material supplying position also can be made as the top of tower 2c of recovery tower 2 and section (section that also comprises concentration tower 1) arbitrarily in addition.
And the 2b of plate column portion (or packed column portion) has the 2e of hydrops portion in the section of regulation.The liquid 10 that the 2e of hydrops portion will flow down from the top accumulates ormal weight at hydrops with shelf 15, makes from hydrops and wanders downwards with the liquid that shelf 15 overflows.In the 2e of hydrops portion, insert tube bank type heat exchanger 8 (with reference to Fig. 4) in the mode that the U-shaped pipe with tube bank type heat exchanger 8 is immersed in the liquid that the 2e of hydrops portion accumulates. Parallel tube portion 8a, 8b in the U-shaped pipe of tube bank type heat exchanger 8 disposes with shelf 15 along hydrops.
The tube portion 8b of the upside in this parallel tube portion is connected with the pipe arrangement 29 (with reference to Fig. 3) of the 2 transmission fluids from concentration tower 1 to recovery tower.Be connected with the pipe arrangement 30 (with reference to Fig. 3) of the 1 transmission fluid from recovery tower 2 to concentration tower at the tube portion 8a of downside.
At this, the effect of the heat exchanger 8 at hydrops portion 2e place is described.
In this device, material liquid flows down by column plate or packed layer from the top of tower 2c of recovery tower 2.This liquid 10 (with reference to Fig. 4) lodges in the 2e of hydrops portion on the hydrops usefulness shelf 15 of section setting arbitrarily.Owing in the 2e of hydrops portion, dispose the U-shaped pipe of tube bank type heat exchanger 8, so this U-shaped pipe is immersed in the liquid 10.Under this state, when the high-temperature vapour in the concentration tower 1 was imported to the tube portion 8b of upside of heat exchanger 8 by pipe arrangement 29, the part of the contacted liquid 10 of outer wall of tube portion 8b, the 8a that moves with high-temperature vapour was heated as steam 18 and rise (with reference to Fig. 4).And the high-temperature vapour that imports from pipe arrangement 29 heat exchanger 8 becomes liquid phase along with mobile and be condensed among the tube portion 8a of downside from the tube portion 8b of upside from gas phase.This liquid is directed to the section (with reference to Fig. 3) of the regulation of concentration tower 1 as described later by the outer pipe arrangement 30 of tower.
Namely, utilize the section of the regulation of pipe arrangement 29 from concentration tower 1 to be connected to the tube portion 8b of the upside of the heat exchanger 8 in the recovery tower 2, and the tube portion 8a that utilizes the downside of the heat exchanger 8 of pipe arrangement 30 from recovery tower 2 is connected to the section of the described regulation in the concentration tower 1, therefore, the HCS in the concentration tower 1 rises in pipe arrangement 29 towards the heat exchanger 8 of recovery tower 2.At this moment, compare with directly flowing up in concentration tower 1, because the pressure loss (flow resistance) in the pipe arrangement 29 is big, so steam is difficult to flow in pipe arrangement 29.Yet, the valve 42 of being located at the 3rd pipe arrangement 30 cuts out and liquid is accumulated in the 3rd pipe arrangement 30, if valve 42 is opened, then the volume steam of liquid enters in the heat exchanger 8, liquid by the 2e of hydrops portion on every side cools off rapidly, produces big volume contraction, therefore, utilize this volume contraction and produce the power that the HCS in the concentration tower 1 is drawn in to the heat exchanger 8 of recoverer 2, thereby can form from concentration tower 1 via pipe arrangement 29 flowing towards the steam of heat exchanger 8.In addition, changing the liquid that comes from steam in heat exchanger 8 flows in the concentration tower 1 because of gravity.Like this, fluid stable ground circulation.Therefore, in the circulation of this fluid, do not need pump equal pressure conveying mechanism.
The concentration tower 1 of present embodiment then, is described.
Be connected with an end of pipe arrangement 26 at the bottommost of the tower bottom 1a of concentration tower 1, the other end of this pipe arrangement 26 is connected with pipe arrangement 27 to the top of tower 2c base feed of recovery tower 2.Because the liquid that makes the tower bottom 1a that accumulates in concentration tower 1 refluxes to the top of tower 2c of the recovery tower 2 that is positioned at the position higher than concentration tower 1, therefore needs to send pump 6 in the way of pipe arrangement 26.
The outside at the top of tower 1c of concentration tower 1 is equipped with the condenser (Ning Shrink device that is called as condenser (コ Application デ Application サ one)) 7, pipe arrangement 28 arranges to condenser 7 from the top, space of top of tower 1c.Therefore, the steam that moves to the top of tower 1c of concentration tower 1 becomes liquid by condenser 7 coolings, thereby obtains being rich in the distillate of the high composition of volatility.And the part of this liquid refluxes to top of tower 1c as required.
And, the 1b of plate column portion (or packed column portion) of concentration tower 1 is communicated with pipe arrangement 29 in the position of regulation, the tube portion 8b of the upside of the heat exchanger 8 that the 2e of hydrops portion that the rising steam in this section is sent at recovery tower 2 by the pipe arrangement 29 that extends along vertical disposes.
In the section of the upside of the section that is inserted with pipe arrangement 29, connect the outer wall of concentration towers 1 and insert from the pipe arrangement 30 of recovery tower 2 sides.Changing the liquid that comes by heat exchanger 8 from steam is imported in the concentration tower 1 by this pipe arrangement 30.And, when the steam that rises in concentration tower 1 is come top of tower 1c, cooled off by condenser 7 by pipe arrangement 28.The result is to obtain being rich in the distillate of the high composition of volatility.
As described above, in the present embodiment, by pipe arrangement 29 steam in the concentration tower 1 is extracted out outside tower, this steam is imported to the heat exchangers 8 in the recovery tower 2, can capture the heat in the concentration tower 1 thus and move it in the recovery tower 2.As present embodiment, used pipe arrangement 29,30 and the hot mobile system of heat exchanger 8 be that section arbitrarily at concentration tower 1 arranges side formula condenser and the structure of side formula reboiler is set in the section arbitrarily of recovery tower 2 simultaneously just.Therefore, compare with the distilling apparatus that does not possess above-mentioned hot mobile system, can reduce concentration tower 1 condenser 7 except heat, also can reduce the hot input quantity of the reboiler 3 of recovery tower 2, the result is to provide a kind of energy efficiency high distilling apparatus.Need to prove, in Fig. 3, show one group of above-mentioned hot mobile system, but the hot mobile system with 10～30% of whole number of theoretical plates suitable group numbers for example can be set.Certainly, the allocation position that number, heat exchanger or pipe arrangement are set of hot mobile system is according to design and arbitrary decision.
In addition, the present patent application people has found, even be not the structure that demarcation strip shown in Figure 2 16 is set as described above in concentration tower 1, also the steam in the concentration tower 1 is extracted out outside tower, the volume contraction that this steam is produced by the heat exchanger 8 whole condensations in the recovery tower 2 becomes driving force, thus obtain from concentration tower 1 to recovery tower 2 so from recovery tower 2 to concentration tower 1 fluid mobile.
According to the present invention, compare with the distilling apparatus of Fig. 2, the such demarcation strip of Fig. 2 16 is not set, correspondingly can reduce the pressure loss in the portion that concentrates 1, reduce concentration tower 1 the tower bottom side pressure and can must be lower with the outlet side pressure restraining of compressor reducer 4.Therefore, energy saving improves.And structure is also simplified.
But, when make owing to the pressure oscillation in the distilling apparatus running etc. with concentration tower 1 in the outlet 30a of the pipe arrangement 30 that is communicated with when becoming not the state that is sealed by liquid, steam can flow in pipe arrangement 30 in concentration tower 1, possibly can't construct flowing of above-mentioned fluid.
In order to prevent this situation, as shown in Figure 3, at the valve 42 that towards the pipe arrangement 30 of concentration tower 1, is provided as the switching mechanism that the pipe arrangement road is opened and closed from the heat exchanger 8 of recovery tower 2.And, being connected with pipe arrangement 44 at the ratio valve 42 of pipe arrangement 30 by upstream side, this pipe arrangement 44 and the low-pressure line (being flare line 43 in this example) with pressure lower than the pressure in the concentration tower 1 link.In this pipe arrangement 44, also be provided with the valve 45 as the switching mechanism that the pipe arrangement road is opened and closed.
When the outlet 30a of pipe arrangement 30 is not sealed by liquid, valve 42 cuts out and valve 45 is opened, forcibly in concentration tower 1, in pipe arrangement 29, introduce steam by the pressure differential between flare line 43 and the concentration tower 1 thus, make the mobile regeneration of above-mentioned fluid.
Owing to come the switching of transfer valve 42 and valve 45 according to the state of the liquid at the outlet 30a place of pipe arrangement 30, therefore preferably in that the position setting that separates of side upstream can monitor the MA monitoring agencies 46 such as liquid level meter that have or not of the liquid in the pipe arrangement from the position of the outlet 30a of pipe arrangement 30.For example, when there is not liquid in the position that MA monitoring agency 46 detects its residing pipe arrangement 30, send signal to the driven for opening and closing portion of valve 42 and valve 45, valve 42 cuts out, valve 45 is opened.Then, as if the existence that confirms liquid by MA monitoring agency 46, then valve 42 is opened, valve 45 is cut out.By this method, in this routine distilling apparatus, can establish the circulation of stable side heat exchange.
Need to prove, as forcibly interior to the pipe arrangement 29 interior mechanisms that introduce steams from concentration tower 1, in the above-described embodiments, be provided with to be connected than the outlet 30a of pipe arrangement 30 and link by the locational pipe arrangement 44 of upstream side with pipe arrangement 44 and have flare line 43, valve 42 and a valve 45 of the pressure lower than the pressure in the concentration tower 1.Yet, realize that the key element of this mechanism is not limited thereto.As long as have than the low pressure of pressure in the concentration tower 1, can not flare line also.And, can be following method: replace valve 42 and valve 45, the direction transfer valve is arranged on the crosspoint of pipe arrangement 30 and pipe arrangement 44, only when confirming liquid pipe arrangement 30 in by MA monitoring agency 46 and use up, utilizes the direction transfer valve only to switch to from pipe arrangement 30 to pipe arrangement 44 mobile paths.In this case, only just can forcibly introduce the mobile regeneration that steam makes fluid in pipe arrangement 29 in concentration tower 1 by the operation of a direction transfer valve, therefore control is simple.
In addition, more than illustrative heat exchange type distilling apparatus of the present invention use the plate column portion identical with common distilling apparatus or packed column portion and constitute, therefore side heat up in a steamer or the enforcement of polynary feeding in need not just improve and can tackle device especially, and the maintenance of installing is also easy.From same reason, owing in the setting of the hop count of concentration tower or recovery tower, have the free degree, therefore also can carry out the optimization of raw material supplying section.That is, as with patent documentation 1 be representative use the problem of heat exchange type distilling apparatus of double-sleeve structure cited described 1)～5) solved by the present invention.
In addition, in the above-described embodiment, owing to use tube bank type heat exchanger 8 as 2 structural elements that carry out the mobile hot mobile system of heat from concentration tower 1 to recovery tower, the therefore pipe design by this heat exchanger 8 and can freely change heat transfer area A.Therefore, about the decision of the heat exchange amount between concentration tower 1 and the recovery tower 2, not only the temperature difference Δ T between concentration tower 1 and the recovery tower 2 also can form heat transfer area A the free degree in the design.According to this situation, used the problem 6 of the heat exchange type distilling apparatus of described double-sleeve structure) solved by the present invention.
About preferred embodiment of the present invention, illustration has also illustrated several embodiments as described above, but the present application is not defined as these embodiments, can carry out various changes certainly and implement in the scope that does not break away from its technological thought.
In the above-described embodiment, show the mode that concentration tower 1 and recovery tower 2 are linked up and down along vertical, but the present invention is not defined as this mode.Namely the present invention includes concentration tower 1 and recovery tower 2 and be respectively independent structures and recovery tower 2 and be configured in the mode of the top when observing from concentration tower 1.
The application advocates that the Japanese publication spy who files an application based on February 24th, 2012 is willing to the priority of 2012-38988, and its disclosed full content is incorporated herein.
Claims (7)
1. heat exchange type distilling apparatus possesses:
Concentration tower, it is utilized as the portion that concentrates and has plate column portion or a packed column portion;
Recovery tower, it is configured in the top when observing from described concentration tower, is utilized and has plate column portion or a packed column portion as recoverer;
First pipe arrangement, it makes the top of tower of described recovery tower be communicated with the tower bottom of described concentration tower;
Compressor reducer, it is arranged at described first pipe arrangement, and the steam from the top of tower of described recovery tower is compressed and transmits to the tower bottom of described concentration tower;
Hydrops portion, its be arranged on described recovery tower regulation the section on, accumulate the liquid that flows down from the top;
Heat exchanger, it is configured in the described hydrops portion of described recovery tower;
Second pipe arrangement, it imports the described heat exchanger of the steam in the described concentration tower to described recovery tower;
The 3rd pipe arrangement, its fluid that will flow out from the described heat exchanger of described recovery tower imports to described concentration tower,
In described heat exchange type distilling apparatus,
Downstream at described the 3rd pipe arrangement links the pipeline with pressure lower than the pressure in the described concentration tower,
Can be with first the flowing and to switch to from described the 3rd pipe arrangement branch and flow towards second of described pipeline in described concentration tower by described the 3rd pipe arrangement.
2. heat exchange type distilling apparatus according to claim 1, wherein,
Also possesses MA monitoring agency, whether this MA monitoring agency monitors in the end that is inserted into described the 3rd pipe arrangement in the described concentration tower and is sealed by liquid, detecting by described MA monitoring agency when not sealed by liquid in this end, flowing described first switches to described second and flows.
3. heat exchange type distilling apparatus according to claim 2, wherein,
Have valve system, this valve system be used for according to the state of the described liquid that is monitored by described MA monitoring agency will described first flow switch to described second mobile.
4. heat exchange type distilling apparatus according to claim 1, wherein,
Also possess the raw material supplying pipe arrangement, this raw material supplying pipe arrangement is to the top of tower base feed of described recovery tower, and/or to the section base feed of the regulation of described plate column portion or packed column portion.
5. heat exchange type distilling apparatus according to claim 4, wherein,
The liquid that also possesses for the tower bottom that will accumulate in described concentration tower carries out pressure-feed pump and pipe arrangement to described raw material supplying pipe arrangement.
6. heat exchange type distilling apparatus according to claim 1, wherein,
The tower bottom of described recovery tower possesses the reboiler that the liquid in this tower bottom is heated.
7. heat exchange type distilling apparatus according to claim 1, wherein,
The top of tower of described concentration tower possesses the condenser that the steam in this top of tower is cooled off.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2012038988A JP5923335B2 (en) | 2012-02-24 | 2012-02-24 | Heat exchange type distillation equipment |
| JP2012-038988 | 2012-02-24 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103285609A true CN103285609A (en) | 2013-09-11 |
| CN103285609B CN103285609B (en) | 2016-01-20 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310043498.5A Active CN103285609B (en) | 2012-02-24 | 2013-02-04 | Heat exchange type distilling apparatus |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US9266034B2 (en) |
| EP (1) | EP2631003B1 (en) |
| JP (1) | JP5923335B2 (en) |
| KR (1) | KR102007629B1 (en) |
| CN (1) | CN103285609B (en) |
| DK (1) | DK2631003T3 (en) |
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| US20120085126A1 (en) * | 2010-10-06 | 2012-04-12 | Exxonmobil Research And Engineering Company | Low energy distillation system and method |
| JP6140591B2 (en) * | 2013-11-21 | 2017-05-31 | 東洋エンジニアリング株式会社 | Distillation equipment |
| DE102015122209A1 (en) * | 2015-12-18 | 2017-02-16 | Basf Se | Column for the thermal treatment of fluid mixtures |
| JP6566876B2 (en) * | 2016-01-26 | 2019-08-28 | 東洋エンジニアリング株式会社 | Heat exchange amount adjustment method for internal heat exchange distillation column |
| CN109107210B (en) * | 2017-06-26 | 2023-11-14 | 河北金牛旭阳化工有限公司 | Rectifying equipment |
| CN109675333B (en) * | 2017-10-19 | 2021-09-14 | 中国石化工程建设有限公司 | Benzene tower fractionation device and method driven by heat pump |
| CN108815874A (en) * | 2018-08-30 | 2018-11-16 | 安徽顺恒信新材料有限公司 | A kind of rectifying still self-flow device |
| CN112742056B (en) * | 2019-10-31 | 2023-01-10 | 中国石油化工股份有限公司 | Internal energy integrated rectifying device for three-component separation and rectifying method using internal energy integrated rectifying device |
| CN112274959A (en) * | 2020-10-24 | 2021-01-29 | 河北工业大学 | Multicomponent disconnect-type rectifying column |
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| JP2011078872A (en) * | 2009-10-05 | 2011-04-21 | National Institute Of Advanced Industrial Science & Technology | Heat exchange type distillation apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| KR20130097667A (en) | 2013-09-03 |
| EP2631003A1 (en) | 2013-08-28 |
| EP2631003B1 (en) | 2015-07-08 |
| DK2631003T3 (en) | 2015-07-27 |
| JP2013173100A (en) | 2013-09-05 |
| JP5923335B2 (en) | 2016-05-24 |
| US9266034B2 (en) | 2016-02-23 |
| KR102007629B1 (en) | 2019-08-06 |
| US20130220791A1 (en) | 2013-08-29 |
| CN103285609B (en) | 2016-01-20 |
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